US3972690A - Gasification process - Google Patents

Gasification process Download PDF

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Publication number
US3972690A
US3972690A US05/608,133 US60813375A US3972690A US 3972690 A US3972690 A US 3972690A US 60813375 A US60813375 A US 60813375A US 3972690 A US3972690 A US 3972690A
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Prior art keywords
reactor
oxygen
fuel
finely dispersed
containing gas
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Expired - Lifetime
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US05/608,133
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English (en)
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George VAN Os
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Shell USA Inc
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Shell Oil Co
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C01B3/363—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents characterised by the burner used

Definitions

  • gas containing substantial amounts of hydrogen and/or carbon monoxide in various mixtures and purities may be used, for instance, as a starting material for the manufacture of chemical products -- e.g., ammonia, alcohols, etc., -- as a reducing agent, as a clean fuel or in hydrogenation processes.
  • a well-known and widely employed method for the preparation of such a gas is the partial combustion of hydrocarbonaceous fuels in a substantially void or hollow reactor.
  • One of the attractive aspects of this process is its flexibility in the types of hydrocarbon fuels which can be converted to the desired gaseous products.
  • Suitable hydrocarbonaceous fuels which may be subject to partial combustion in this non-catalytic process include normally gaseous and liquid hydrocarbons, e.g., middle distillates and light and heavy fuel oil, as well as liquid fuels mixed with solid carbon-containing particles such as the carbon soot typically obtained as a product of partial combustion.
  • the combustion can be effected with oxygen, with air, or with air which has been enriched with oxygen. Frequently steam is added to the reaction mixture.
  • a frequently used hydrocarbonaceous fuel is a residual petroleum fraction which fuel contains ash-forming constituents.
  • the percentage of ash is relatively low, i.e., generally not exceeding 0.05% weight, and in the conventional hollow reactors such an ash content presents no difficulties.
  • the ash particles thus formed leave the reactor with the product gases and are separated from the gases by means known in the art, before, after or during cooling of the gases.
  • hydrocarbonaceous fuels employed contain more than about 0.1%w finely dispersed solids.
  • Liquid petroleum fractions with a far higher content of finely dispersed solids is obtained, for instance, from the mining and processing of tar sands. These tar sand deposits occur in very large deposits at various places on earth and present potentially valuable sources of petroleum.
  • liquid petroleum fractions are obtained with a solids content varying typically from about 0.5 to about 5.0% weight. These solids consist mainly of sand and clay particles.
  • Another source of high solid content hydrocarbonaceous fuel employed in partial combustion processes is a liquid petroleum fraction containing a dispersion of coal, soot or coke.
  • the coal may be hard coal, such as anthracite, or bituminous coal, brown coal or lignite.
  • Such dispersions of solid particles in liquid petroleum fractions are useful fuels in partial combustion processes because it is a convenient means of pressurizing solid fuel in a reactor in order to gasify the solid and liquid fuel.
  • the solid particles, in particular the various type of coal typically contain ash-forming constituents.
  • the oxidant-air, oxygen or a mixture of the two are introduced into the reaction chamber in such a fashion that the oxidizing gas is rotated tangentially around the injected finely dispersed fuel in order to promote the stability of the flare. See, for example, British Pat. No. 1,116,979. Further, the oxidant is given this strong rotary motion because this also promotes swirling of the reaction mixture in the reactor and consequently improves the mixing of fuel and oxidant. A result of this strong swirling action in the reactor is that the solid particles in the feed are flung against the wall of the reactor. As long as these particles are hard and non-sticky, there is little problem of deposits and accumulation.
  • the reaction mixture in the reactor has an outward swirl in which a relatively large amount of partly combusted oil is still present, especially in the middle and upper part of the reactor where deposits can be formed.
  • One measure in the degree of swirl within the reactor is the ratio of the axial velocity component (V ax ) of the oxidant as compared to the tangential velocity compounds (V tan ) of the oxidant as measured at the outlet of the injection device.
  • V ax the ratio of V ax to V tan is typically less than 2, resulting in such a degree of outward swirl of the reaction mixture in the reactor as to create deposits on the reactor walls.
  • the present invention is an improvement in the process for the partial combustion of a liquid hydrocarbon fuel containing finely dispersed solids in a substantially void reactor wherein the fuel is mixed with or finely dispersed in an oxygen-containing gas and passed as a solid-containing gaseous jet through at least one supply opening in the reactor and wherein the oxygen-containing gas is introduced into the reactor with an axial as well as tangential velocity component so as to impart a swirl to the flame, which improvement comprises maintaining the ratio of the axial velocity component (V ax ) of the oxygen-containing gas as compared to the tangential velocity component (V tan ) of the oxygen-containing gas in excess of 3.0, preferably 4 to 5.
  • the apparatus comprises a substantially void reactor having an inlet device with a central tube for the supply of the fuel surrounded by an inlet channel for the oxidant, the center line of the tube and the channel coinciding with the center line of the reactor, the inlet channel being provided with a tangentially directed supply tube for the oxidant, while the ratio of the diameter of the channel for the oxidant to the diameter of the output opening of that channel is at least 3.
  • the oxidant is forced to flow through a relatively more narrow opening than found in conventional design whereby the axial component of the velocity is increased.
  • FIG. 1 is a longitudinal section of an apparatus according to the invention.
  • FIG. 2 shows in more detail a longitudinal section in which such an apparatus is compared with an apparatus according to prior art.
  • the partial combustion step of the present invention can be suitably carried out using air, oxygen-enriched air or oxygen as the oxidant source (oxygen-containing gas).
  • the reaction will be conducted under conditions of temperature and pressure such that the reaction is self-supporting.
  • the reaction temperature broadly stated, is from about 700° to about 2000°C with a reaction pressure of from atmospheric to about 600 psig.
  • the reaction temperature and pressure are preferably 900°-1400°C and atmospheric to 30 psig, respectively, when air is used as the oxidant source with somewhat higher temperatures and pressures, e.g., 1100°-1700°C and atmospheric to 600 psig, being employed when oxygen is used as the source of oxygen-containing gas.
  • suitable hydrocarbonaceous fuels include those mentioned in the section of the specification entitled Background of the Invention.
  • liquid hydrocarbon or petroleum fractions include gasoline, kerosene, naphtha, distillates, gas oils and residual oils.
  • a particularly preferred feed to be employed in the present invention is the petroleum fraction obtained from the processing of tar sands.
  • the O/C ratio (oxygen to carbon) of the total oxygen-containing gas and hydrocarbonaceous fuel feedstock introduced into the partial combustion reaction zone may suitably vary between about 0.8 and about 2.0 with ratios in the range of 0.8 to about 1.2 being preferred.
  • Certain benefits are also realized in the process when steam is introduced into the reactor with either or both of the hydrocarbon fuel and/or oxygen-containing gas feedstock to the partial combustion reactor.
  • the oxygen-containing gas, the hydrocarbonaceous fuel or the oxygen-containing gas/hydrocarbonaceous fuel admixture may be mixed with steam or passage into the partial combustion reactor.
  • either or both of the hydrocarbonaceous fuel and oxygen-containing gas feedstreams may be subject to preheating via external heat exchange prior to introduction into the partial combustion reactor.
  • the apparatus suitable for carrying out the process according to the invention comprises a substantially void reactor having an inlet device with a central tube for the supply of the fuel surrounded by an inlet channel for the oxygen-containing gas, the center lines of the tube and the channel coinciding with the center line of the reactor, the inlet channel being provided with a tangentially directed supply tube for the oxygen-containing gas, while the ratio of the diameter of the channel for the oxidant to the diameter of the outlet opening of that channel is at least 3.
  • an inlet device of current dimensions suitable for the gasification of oil to the gasification of liquid hydrocarbons containing finely dispersed solids. This may be done by applying a thin coating of a suitable metal, e.g., steel, to the inside of the channel for the oxidant near the outlet opening.
  • a suitable metal e.g., steel
  • a reactor with a conventional length to width ratio of about 2 to 3 gives excellent performance. If desired, a reactor with a larger length to width ratio may be employed and be adapted to the length of the flame.
  • the center line of it preferably coincides with the center line of the reactor. If a plurality of supply devices are present, they are preferably arranged in a regular array relative to the center line of the reactor, the distance between any two supply devices being at least 10 times as large as the diameter of the outlet of the supply device and the diameter of the reactor being so large that the distance between the wall of the reactor and the nearest supply device is at least five times as large the diameter of the outlet of the supply device.
  • the inlet device 2 contains a central pipe or tube 3 for supply of the liquid hydrocarbon feed which liquid feed contains finely dispersed solids.
  • This central tube 3 is surrounded by a channel 4 for the oxygen-containing gas, which gas may or may not be mixed with steam.
  • the channel 4 is connected to a tangentially directed oxidant supply tube 5 such that the oxidant from supply tube 5 rotates around fuel tube 3 in the direction of outlet 6.
  • the ratio of the diameter D of channel 4 to diameter d of outlet 6 is significant since as this ratio is increased, the gaseous oxidant-fuel mixture will enter the reaction chamber with a larger axial component of the velocity.
  • a typical ratio of D to d according to the present invention is about 4.5 as compared to a value of less than about 3 for a conventional design.
  • the inlet device is furthermore provided with a water jacket 7 having an inlet 8 and outlet 9 for the circulating cooling water.
  • FIG. 2 indicates how a conventional inlet device may be adapted for use in the present invention.
  • the lefthand side of FIG. 2 shows a conventional inlet device whereas the righthand side shows a conventional inlet device modified for use in the present invention.
  • D 1 , D 2 , d 1 and d 2 denote the diameters in accordance with D and d of FIG. 1. Parts 10 and 11 have the same dimensions and diameter D 1 equals diameter D 2 . It has been shown in FIG. 2 that by applying a coating 12 of a suitable steel and by a minor modification of the lining 13 of the nozzle of the inlet device, that diameter d 2 has been made smaller than diameter d 1 and consequently D 2 /d.sub. 2 ⁇ D 1 /d 1 .
  • “Ash retention” is the difference between the amount of ash introduced into the reactor with the fuel and the amount of ash leaving the reactor with the gas, expressed as a percentage of the ash present in the feed. After run 3, a 25 mm thick layer of porous ash was found to be adhering to the top and to the side wall down to about the middle of the reactor. The temperature in the reactor was invariably lower than the melting point of the ash present in the feed (about 1320°C).

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US05/608,133 1974-09-09 1975-08-27 Gasification process Expired - Lifetime US3972690A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL7411916 1974-09-09
NLAANVRAGE7411916,A NL179468C (nl) 1974-09-09 1974-09-09 Werkwijze voor het vergassen van olie door partiele oxydatie onder tangentiele invoer van de oxydant.

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US3972690A true US3972690A (en) 1976-08-03

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US05/608,133 Expired - Lifetime US3972690A (en) 1974-09-09 1975-08-27 Gasification process

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US (1) US3972690A (de)
JP (1) JPS593921B2 (de)
BE (1) BE832882A (de)
CA (1) CA1070949A (de)
DD (1) DD120464A5 (de)
DE (1) DE2539888C2 (de)
FR (1) FR2283859A1 (de)
GB (1) GB1523341A (de)
IN (1) IN142330B (de)
IT (1) IT1042368B (de)
NL (1) NL179468C (de)
ZA (1) ZA755705B (de)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3977365A (en) * 1973-08-06 1976-08-31 Vierling Donald E Method of oxidizing fuels
US4241656A (en) * 1978-11-17 1980-12-30 Smith R. P. M. Corporation Self-cleaning nozzle for lithographic printing dampeners
US4338099A (en) * 1979-12-26 1982-07-06 Texaco Inc. Process for the partial oxidation of slurries of solid carbonaceous fuels
US4351647A (en) * 1980-07-14 1982-09-28 Texaco Inc. Partial oxidation process
US4352675A (en) * 1979-11-30 1982-10-05 Ruhrkohle Aktiengesellschaft Coal gasification reactor
US4364744A (en) * 1979-12-26 1982-12-21 Texaco Inc. Burner for the partial oxidation of slurries of solid carbonaceous fuels
US4386941A (en) * 1979-12-26 1983-06-07 Texaco Inc. Process for the partial oxidation of slurries of solid carbonaceous fuel
US4400180A (en) * 1980-12-03 1983-08-23 Texaco, Inc. Partial oxidation process
US4566880A (en) * 1978-11-30 1986-01-28 Ruhrkohle Ag Reactor for coal gasification
FR2648800A1 (fr) * 1989-06-27 1990-12-28 Inst Francais Du Petrole Dispositif et procede de fabrication de gaz de synthese par combustion et son application
US4999029A (en) * 1989-01-31 1991-03-12 Pasf Aktiengesellschaft Preparation of synthesis gas by partial oxidation
US5006062A (en) * 1986-05-12 1991-04-09 Institute Of Gas Technology Treatment of solids in fluidized bed burner
US6775984B2 (en) * 2000-11-21 2004-08-17 Snecma Moteurs Full cooling of main injectors in a two-headed combustion chamber
WO2009139894A1 (en) * 2008-05-15 2009-11-19 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US20100251614A1 (en) * 2009-04-01 2010-10-07 Conocophillips Company Two stage dry feed gasification system and process
US9561483B2 (en) 2011-05-10 2017-02-07 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and reactor for producing synthesis gas

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2851704A1 (de) * 1978-11-30 1980-06-12 Ruhrkohle Ag Reaktor fuer kohlevergasungsverfahren
DE3242699C1 (de) * 1982-11-19 1984-07-19 Bergwerksverband Gmbh, 4300 Essen Verfahren zur autothermen Vergasung von festen und flüssigen Brennstoffen im Flugstrom
US4952218A (en) * 1988-08-26 1990-08-28 The Dow Chemical Company Two-fluid nozzle for atomizing a liquid solid slurry and protecting nozzle tip
DE19929945C1 (de) * 1999-06-29 2001-03-01 Daimler Chrysler Ag Reaktandzufuhrsystem und dieses verwendendes Reaktandzufuhrverfahren

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1826776A (en) * 1928-07-20 1931-10-13 Charles O Gunther Liquid fuel burner and method of atomizing liquids
US2535730A (en) * 1947-10-08 1950-12-26 Gascogne Papeteries Process for the treatment of waste liquors derived from cellulose manufacture
GB815451A (en) * 1956-10-31 1959-06-24 Bataafsche Petroleum Improvements in or relating to combustion apparatus
US2904417A (en) * 1959-09-15 Process for the production of synthesis
US2971829A (en) * 1958-12-23 1961-02-14 Shell Oil Co Hydrocarbon gasification
US3272441A (en) * 1965-11-03 1966-09-13 Gulf Research Development Co Aspirating spray nozzle
GB1116979A (en) 1964-07-07 1968-06-12 Montedison Spa Apparatus for the partial combustion of a liquid fuel
US3528930A (en) * 1968-05-29 1970-09-15 Texaco Inc Production of synthesis gas

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2790838A (en) * 1952-01-16 1957-04-30 Eastman Kodak Co Process for pyrolysis of hydrocarbons
DE968064C (de) * 1952-01-23 1958-01-16 Koppers Gmbh Heinrich Verfahren und Vorrichtung zum Erzeugen wertvoller, Kohlenoxyd und Wasserstoff enthaltender Gase
US3758037A (en) * 1971-10-04 1973-09-11 Texaco Development Corp Fuel burner and process for gas manufacture

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2904417A (en) * 1959-09-15 Process for the production of synthesis
US1826776A (en) * 1928-07-20 1931-10-13 Charles O Gunther Liquid fuel burner and method of atomizing liquids
US2535730A (en) * 1947-10-08 1950-12-26 Gascogne Papeteries Process for the treatment of waste liquors derived from cellulose manufacture
GB815451A (en) * 1956-10-31 1959-06-24 Bataafsche Petroleum Improvements in or relating to combustion apparatus
US2971829A (en) * 1958-12-23 1961-02-14 Shell Oil Co Hydrocarbon gasification
GB1116979A (en) 1964-07-07 1968-06-12 Montedison Spa Apparatus for the partial combustion of a liquid fuel
US3272441A (en) * 1965-11-03 1966-09-13 Gulf Research Development Co Aspirating spray nozzle
US3528930A (en) * 1968-05-29 1970-09-15 Texaco Inc Production of synthesis gas

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3977365A (en) * 1973-08-06 1976-08-31 Vierling Donald E Method of oxidizing fuels
US4241656A (en) * 1978-11-17 1980-12-30 Smith R. P. M. Corporation Self-cleaning nozzle for lithographic printing dampeners
US4566880A (en) * 1978-11-30 1986-01-28 Ruhrkohle Ag Reactor for coal gasification
US4352675A (en) * 1979-11-30 1982-10-05 Ruhrkohle Aktiengesellschaft Coal gasification reactor
US4338099A (en) * 1979-12-26 1982-07-06 Texaco Inc. Process for the partial oxidation of slurries of solid carbonaceous fuels
US4364744A (en) * 1979-12-26 1982-12-21 Texaco Inc. Burner for the partial oxidation of slurries of solid carbonaceous fuels
US4386941A (en) * 1979-12-26 1983-06-07 Texaco Inc. Process for the partial oxidation of slurries of solid carbonaceous fuel
US4351647A (en) * 1980-07-14 1982-09-28 Texaco Inc. Partial oxidation process
US4400180A (en) * 1980-12-03 1983-08-23 Texaco, Inc. Partial oxidation process
US5006062A (en) * 1986-05-12 1991-04-09 Institute Of Gas Technology Treatment of solids in fluidized bed burner
US4999029A (en) * 1989-01-31 1991-03-12 Pasf Aktiengesellschaft Preparation of synthesis gas by partial oxidation
EP0406071A1 (de) * 1989-06-27 1991-01-02 Institut Français du Pétrole Vorrichtung und Verfahren zur Herstellung von Synthesegas durch Verbrennung und seine Anwendung
FR2648800A1 (fr) * 1989-06-27 1990-12-28 Inst Francais Du Petrole Dispositif et procede de fabrication de gaz de synthese par combustion et son application
US6775984B2 (en) * 2000-11-21 2004-08-17 Snecma Moteurs Full cooling of main injectors in a two-headed combustion chamber
WO2009139894A1 (en) * 2008-05-15 2009-11-19 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US20110162275A1 (en) * 2008-05-15 2011-07-07 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US8430939B2 (en) 2008-05-15 2013-04-30 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US9243197B2 (en) 2008-05-15 2016-01-26 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US20100251614A1 (en) * 2009-04-01 2010-10-07 Conocophillips Company Two stage dry feed gasification system and process
US8357216B2 (en) 2009-04-01 2013-01-22 Phillips 66 Company Two stage dry feed gasification system and process
US9140447B2 (en) 2009-04-01 2015-09-22 Lummus Technology Inc. Two stage dry feed gasification process
US9175847B2 (en) 2009-04-01 2015-11-03 Lummus Technology Inc. Two stage dry feed gasification system
US9561483B2 (en) 2011-05-10 2017-02-07 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and reactor for producing synthesis gas

Also Published As

Publication number Publication date
IT1042368B (it) 1980-01-30
GB1523341A (en) 1978-08-31
NL179468B (nl) 1986-04-16
BE832882A (nl) 1976-03-01
FR2283859B1 (de) 1978-04-07
DD120464A5 (de) 1976-06-12
DE2539888C2 (de) 1985-07-18
AU8462275A (en) 1977-03-17
CA1070949A (en) 1980-02-05
NL179468C (nl) 1986-09-16
ZA755705B (en) 1976-08-25
FR2283859A1 (fr) 1976-04-02
IN142330B (de) 1977-06-25
DE2539888A1 (de) 1976-03-18
JPS5159901A (de) 1976-05-25
JPS593921B2 (ja) 1984-01-26
NL7411916A (nl) 1976-03-11

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